CN109661408A - The method for producing polymer using the compound comprising at least two unsaturation carbon-carbon bond - Google Patents
The method for producing polymer using the compound comprising at least two unsaturation carbon-carbon bond Download PDFInfo
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- CN109661408A CN109661408A CN201780054001.6A CN201780054001A CN109661408A CN 109661408 A CN109661408 A CN 109661408A CN 201780054001 A CN201780054001 A CN 201780054001A CN 109661408 A CN109661408 A CN 109661408A
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F6/00—Post-polymerisation treatments
- C08F6/001—Removal of residual monomers by physical means
- C08F6/003—Removal of residual monomers by physical means from polymer solutions, suspensions, dispersions or emulsions without recovery of the polymer therefrom
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2/00—Processes of polymerisation
- C08F2/01—Processes of polymerisation characterised by special features of the polymerisation apparatus used
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F36/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, at least one having two or more carbon-to-carbon double bonds
- C08F36/02—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, at least one having two or more carbon-to-carbon double bonds the radical having only two carbon-to-carbon double bonds
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- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Polymerisation Methods In General (AREA)
Abstract
The present invention relates to use the compound comprising at least two unsaturation carbon-carbon bond the method that produces polymer, wherein the method includes polymeric segments and purification section, wherein the product of the polymeric segment is subjected to including a series of purification steps below in the purification section: vapor phase is removed from the product of the polymeric segment by flash separation, to obtain the first vapor phase and polymerizate；Make first vapor phase through compressed and condensation process, to obtain the second vapor phase and through condensed monomer phase；Wherein the purification step carries out in the order.This method allows the optimal utilization of the raw material in the polymerization.
Description
A kind of compound the present invention relates to use comprising at least two unsaturation carbon-carbon bond is come the method that produces polymer.
The invention further relates to the polymer produced according to the method.
In polymerization, the optimal utilization of raw material is a very important aspect.For many reasons, including environment
Consideration and economic cause, it may be desirable to strive for making raw material farthest be converted to value product in polymerization.
Moreover, it is often desirable for striving for that raw material is made farthest to be converted to specific special product, to avoid the need for removal by-product
Separating step and required final product is obtained from method.
However, polymerization usually has part material and does not translate into this property of required polymer product.This can
The property chemically reacted can be for example attributed to.
One this polymerization is poly- to produce by polymerizeing the compound comprising at least two unsaturation carbon-carbon bond
Close object.The example of this kind of compound includes butadiene.In the method for producing polybutadiene by making polymerizing butadiene, poly-
It closes in section and carries out polymerization process.Polymeric segment generates the product mixtures comprising part required product and part unreacting material.
The product mixtures obtained from polymeric segment can be subjected to separating step, such as flash separation step, carry out isolating polymer
Product and vapor phase.In flash separation operation, the product mixtures with given pressure are introduced into pressure and are mixed lower than product
Object is fed to the container of pressure locating for container.The pressure subtracted drops due to this, and the partial material in product mixtures will steam
Hair forms vapor phase.In addition part will not evaporate and will form liquid phase or solid phase.
Flash separation container is that the field of production polymer material is well-known.The product obtained from polymeric segment can be mixed
It closes object and introduces flash separation container via one or more entrances for example in flash separation container side wall.Polymer product
Solid phase can be formed, and can for example be removed from flash chamber via outlet at bottom.The steam that can will be obtained by flashing operation
It is mutually for example removed from flash chamber via top exit, forms the first vapor phase.
Flashing operation can be carried out for example with the pressure drop of≤300kPa, such as≤250kPa, preferably 50-300kPa.Pressure drop is
The difference being introduced between the pressure in the pressure and flash chamber of the product mixtures of flash chamber.For example, introducing flash chamber
Product mixtures pressure can >=200kPa, such as 200-400kPa.
The vapor phase for a certain amount of raw material that this flash separation generation is not consumed during including polymerization reaction.It is expected that
Be to strive for making the feedstock recycle from the vapor phase that flash separation obtains.This raw material may include unreacted comprising at least
The compound of 2 unsaturated carbon-carbon bonds, such as unreacted butadiene.
This is according to the present invention by using the production of chemicals polymer comprising at least two unsaturation carbon-carbon bond
Method realizes, wherein the method includes polymeric segment and purification section, wherein the product of polymeric segment be subjected in purification section include
A series of purification steps below:
Vapor phase is removed from the product of polymeric segment by flash separation, to obtain the first vapor phase and polymerizate；
Make the first vapor phase through compressed and condensation process, to obtain the second vapor phase and through condensed monomer phase；
Wherein purification step carries out in the order.
Particularly preferably the compound comprising at least two unsaturation carbon-carbon bond is selected from butadiene, pentadiene, hexadiene, heptan two
Alkene, octadiene or their combination.Most preferably, the compound comprising at least two unsaturation carbon-carbon bond is 1,3-butadiene.
Can be supplied to the raw material flow of polymeric segment to be converted to the raw material in the vapor phase from flash separation, need by
Raw material is extracted and converted to liquid form from vapor phase.This extraction and conversion can by making the first vapor phase through compressed and
Condensation process carries out.This compression and condensation process can produce through condensed monomer phase and the second vapor phase.Through condensed monomer phase
It may include unreacted raw material, such as butadiene.It goes forward side by side from compression with what condensation process obtained through condensed monomer is mutually recyclable
Expect to polymeric segment.
Compression can be carried out for example in compressor, such as liquid-piston compressor.Alternatively, more than one compression can be used
Machine.Specifically, this compressor can be gas compressor.Accommodable representative gases compressor is positive displacement compressor, packet
Include rotary screw machine, rotary vane compressor and liquid-piston compressor.Specifically, liquid-piston compressor is suitable for pressing
Contract the first vapor phase obtained in the method according to the invention.
This kind of liquid-piston compressor generally includes tubular discharge chambe, and wherein rotor is disposed offset from position.There are liquid,
Along the inner wall forming layer of cylinder during rotor motion.Water is particularly preferably used as liquid to operate liquid-piston compressor to be formed
Liquid level.Rotor generally includes axis and blade (blade is connected to rotor, is longitudinally connected to axis), including the opening between blade
Space.These open spaces are usually sealed by liquid level during rotation process.Due to the deviation post of rotor, open space
Volume is gradually reduced and increases again.Settable one or more gas access, so that gas is to fill with maximum volume
The mode of one or more open spaces enters discharge chambe.The gas being fed into discharge chambe is preferably the first vapor phase.Pass through
Rotation, the volume that gas enters open space reduces, and therefore makes gas compression.One or more gas vents are preferably provided with,
So that it allows gas the smallest rotor-position of the volume of open space between blade and liquid level to leave discharge chambe.Pendular ring type
Compressor can be single-stage or multistage.Compound compressor can have such as two compression stages on common axis.
Typical liquid-piston compressor is for example described in ' Liquid Ring Vacuum Pumps, Compressors and
In Systems ', H.Bannwarth, ISBN:978-3-527-31249-8.
In the operation of this liquid-piston compressor, condition in discharge chambe preferably so that be used to be formed the liquid of liquid level
Amount it is sufficiently high to ensure required compression, but cannot be excessively high to avoid the efficiency for reducing compressor.
Preferably, compression step includes that the first vapor phase is compressed to >=the pressure of 400kPa.Leave compressor through pressing
Contracting vapor phase can such as pressure with >=400kPa, more preferably >=500kPa, more preferably >=500kPa and≤1.0MPa.
That leaves compressor mutually can be subjected to condensation process and being fed into condenser through compressed vapour.This condenser can
For the shell and tube heat exchanger for example with cooling water charging.It can be obtained from condenser through condensed monomer phase and not condensable phase.
It mutually can be subjected to separating in decanter through condensed monomer.This decanter can be such as slot.Using Pendular ring type pressure
Contracting machine is come in the case where compressing the first vapor phase, liquid, such as water from Pendular ring type reactor can fall to the bottom of decanter
In portion, liquid-piston compressor is returned to wherein can remove it and feed.Through being separated in condensed monomer Xiang Kecong decanter.Through condensing
Monomer is mutually optionally subjected to purification process.Polymeric segment is returned to through condensed monomer is mutually recyclable.
Not condensable phase is also referred to as the second vapor phase, can be subjected in addition in another embodiment of method of the invention
Purification process, wherein the second vapor phase is subjected to absorption step and stripping step to obtain second comonomer phase.Absorption step is preferred
It is carried out in >=the pressure of 300kPa, such as >=300kPa and≤550kPa.
Absorption step can carry out in filling column separator.Preferably, filling column separator is disposed vertically, and having will
For mineral oil feedstock to the entrance above the filled section of tower of tower, the second vapor phase enters the entrance of tower, and from tower
Except the outlet positioned at bottom of the mineral oil containing the compound comprising at least two unsaturation carbon-carbon bond absorbed.Mineral oil
Can tower for example be fed into 40-60 DEG C, preferably 45-55 DEG C of temperature.
In preferred embodiments, absorption step carries out in the filling column separator being disposed vertically, the separator
There is the entrance above the filled section of tower, wherein by the mineral oil feedstock with 45-55 DEG C of temperature to tower；And it is located at bottom
The outlet in portion, wherein mineral oil of the removal containing the compound comprising at least two unsaturation carbon-carbon bond absorbed from tower.
Preferably, the second vapor phase enters tower via the entrance below the filled section for being located at tower.
Mineral oil preferably synthesizes isoparaffin.Preferably, mineral oil has≤30 weight %, more preferably≤20 weight %
Arene content.It is further preferred that mineral oil have measured according to ISO 1523 (2002) >=40 DEG C of flash-point.Particularly preferred mine
Object oil be arene content with≤20 weight % and according to ISO 1523 (2002) measurement >=synthesis of 40 DEG C of flash-point
Isoparaffin.Further preferred mineral oil is C10-C12 mineral oil, such as contains 10-12 carbon comprising at least 98 weight %
The mineral oil of the molecule of atom.It can help to prevent to take with the compound comprising at least two unsaturation carbon-carbon bond using this oil
Band mineral oil.
In the preferred embodiment of absorption step operation, mineral oil is defeated to flow downward along the filled section of filling column separator
It send, and the second vapor phase is conveyed along the filled section of filling column separator with flowing up, so that mineral oil and second steams
Gas phase is along filled section counter-current flow.Absorption step facilitates absorption efficiency operate in this way.
In embodiments of the invention, absorption step includes that will inhale comprising the compound of at least two unsaturation carbon-carbon bond
It closes in mineral oil, and stripping step includes the compound that separation includes at least two unsaturation carbon-carbon bond from mineral oil.
Preferably, stripping step is carried out in the pressure of≤600kPa.Further preferably stripping step is carried out in≤70 DEG C of temperature.Particularly preferably
Stripping step is carried out in the pressure of≤600kPa and≤70 DEG C of temperature.
Stripping step can be carried out for example in the filling column separator that is disposed vertically of the bottom of tower equipped with reboiler.
Second comonomer phase can be obtained from stripping step.This second comonomer is mutually recyclable to return to polymeric segment.
It in certain embodiments, can be according to the method for the present invention continuous process, wherein polymeric segment is grasped in a continuous manner
Make and purification section operates in a continuous manner.In such an implementation, the recycling through condensed monomer phase can be carried out directly；Substitution
Ground, from compression and condensation process obtain through condensed monomer mutually can in polymeric segment further utilize before completely or partially deposited
Storage.
It particularly preferably according to the method for the present invention include making at least 95 weight %, more preferably at least 98 weight %, even more
The monomer conversion comprising at least two unsaturation carbon-carbon bond for being introduced to polymeric segment of preferably at least 99 weight %.
Alternatively, the invention also includes scheme is implemented as follows: wherein polymerization includes by making comprising at least two insatiable hunger
It polymerize with the compound of carbon-carbon bond to produce polymer, wherein the compound comprising at least two unsaturation carbon-carbon bond is 1,3-
Butadiene.It preferably, according to the method for the present invention include making at least 95 weight %, more preferably at least 98 weight %, even more excellent
The 1,3- butadiene conversion for being introduced to polymeric segment of choosing at least 99 weight %.
Polymeric segment may include single reactor, or alternatively multiple reactors.
Segregation section can receive product mixtures for separating from single reactor or multiple reactors.
The invention further relates to certain embodiments, and wherein polymeric segment includes multiple reactors with batch operation to operate,
Wherein the product mixtures from these batch reactors are fed to segregation section, and wherein segregation section is operated with operating continuously.
In particularly preferred embodiments, the present invention relates to use the chemical combination comprising at least two unsaturation carbon-carbon bond
Object, i.e. 1,3-butadiene be the method that produces polymer, wherein the method includes polymeric segment and purification section, wherein polymeric segment
Product is subjected to including a series of purification steps below in purification section:
Vapor phase is removed from the product of polymeric segment by flash separation, to obtain the first vapor phase and polymerizate,
Wherein the pressure drop in flash separation is 50-300kPa；And
It is subjected to the first vapor phase in liquid-piston compressor to the compression of the pressure of >=400kPa and cold being used as
Condensation process in the shell and tube heat exchanger with cooling water charging of condenser, to obtain the second vapor phase and through condensed monomer
Phase；
Wherein purification step carries out in the order, and is wherein mutually recycled back into polymeric segment through condensed monomer.
It it is also especially preferred to be related to a kind of compound of the use comprising at least two unsaturation carbon-carbon bond, i.e. 1,3- fourth two
Alkene produces embodiment of the present invention of the method for polymer, wherein the method includes polymeric segments and purification section, wherein gathering
The product for closing section is subjected to including a series of purification steps below in purification section:
Vapor phase is removed from the product of polymeric segment by flash separation, to obtain the first vapor phase and polymerizate,
Wherein the pressure drop in flash separation is 50-300kPa；And
It is subjected to the first vapor phase in liquid-piston compressor to the compression of the pressure of >=400kPa and cold being used as
Condensation process in the shell and tube heat exchanger with cooling water charging of condenser, to obtain the second vapor phase and through condensed monomer
Phase；
Wherein purification step carries out in the order, and is wherein mutually recycled back into polymeric segment through condensed monomer；
It is wherein single to obtain second the method further includes making the second vapor phase be subjected to absorption step and stripping step
Body phase；
Wherein absorption step is carried out in the pressure of >=300kPa and≤550kPa；
Wherein absorption step carries out in the filling column separator being disposed vertically, and the separator has mineral oil feedstock
To the entrance above the filled section of tower of tower, the mineral oil is that have the arene content of≤20 weight % and according to ISO
1523 (2002) measurement >=the synthesis isoparaffin of 40 DEG C of flash-point, and with 45-55 DEG C of temperature；Second vapor phase into
Enter the entrance of tower；And the outlet positioned at bottom, wherein being removed from tower containing what is absorbed includes at least two unsaturated carbon-
The mineral oil of the compound of carbon key；
Wherein stripping step includes being disposed vertically in filling column separator equipped with reboiler in the bottom of tower ,≤
The pressure of 600kPa and≤70 DEG C of temperature, separation includes the compound of at least two unsaturation carbon-carbon bond from mineral oil；
Wherein second comonomer is mutually recycled back into polymeric segment.
Specific embodiments of the present invention are illustrated in Fig. 1 and 2.Fig. 1 is presented according to the method for the present invention, including by unit
The polymeric segment that I is indicated and the purification section indicated by unit II, III and IV, wherein unit II is flash separation container, unit
III is compressor and unit IV is condenser, obtains from unit IV through condensed monomer phase F, returns to polymeric segment by feeding.
The embodiment of Fig. 1 is presented according to the method for the present invention in Fig. 2, further comprise make the second vapor phase G be subjected to by
The absorption step and the stripping step indicated by unit VI that unit V is indicated, to obtain the second comonomer phase that charging returns to polymeric segment.
In Fig. 1:
Material stream A indicates the reaction mixture for containing the compound comprising at least two unsaturation carbon-carbon bond；
Unit I indicates polymeric segment；
The product of material stream B expression polymeric segment；
Unit II, III and IV indicate purification section, and wherein unit II indicates flash separation container；
Material stream C indicates the separated polymerizate of flash separation；
Material stream D indicates the first vapor phase obtained from flash separation container；
Unit III indicates compressor；
Material stream E indicates compressed first vapor phase；
Unit IV indicates condenser；
Material stream F indicates to return to polymeric segment by feeding through condensed monomer phase；And
Material stream G indicates the second vapor phase.
It in a more particular embodiment, according to the method for the present invention further comprise absorption step and stripping step.Fig. 2
Present the disclosure of embodiment of the present invention including this absorption step and stripping step, in which:
Unit V indicates absorptive unit；
Material stream H indicates absorbing medium；
Material stream J indicates the absorbing medium comprising institute's absorption compound；
Unit VI indicates steam stripping unit；
Material stream K indicates waste streams；And
Material stream L indicates second comonomer phase, returns to polymeric segment by feeding.
The present invention is now illustrated by following non-limiting embodiment.
In the polymeric segment I for including polymer reactor, the reaction comprising 16913kg 1,3-butadiene and 24000kg water is mixed
It closes object A to react in batch operation, includes polybutadiene and 868kg 1 of the 16045kg as polymerizate, 3- fourth two to obtain
The material stream B of alkene.Material stream B is fed into flash separation container II in 63 DEG C of temperature and the pressure of 348kPa.From flash distillation point
From in container, acquisition is in 61 DEG C of temperature and the pressure of 376kPa, includes 16045kg polymerizate and 43kg 1,3- fourth two
The material stream C of alkene, and acquisition is in 53 DEG C of temperature and the pressure of 121kPa, includes 825kg 1,3-butadiene and 16kg water
The first vapor phase of expression material stream D.
In the pressure of 121kPa and 53 DEG C of temperature, with the rate of 2162kg 1,3-butadiene and 43kg water by material stream D
It is fed into compressor III.Material stream E leaves compressor in the pressure of 445kPa and 20 DEG C of temperature, and in these pressure and
Condenser IV is entered with the rate of 2162kg 1,3- butadiene and 43kg water under the conditions of temperature.It is in from condenser
The material stream F of the pressure of 575kPa and 20 DEG C of temperature, 1,3-butadiene comprising 1788kg/h recycling, it is recyclable to be used for
In polymeric segment I, and in 20 DEG C temperature and 445kPa pressure, comprising 374kg/h 1,3-butadiene and 43kg/h water
Indicate the material stream G of the second vapor phase.
Compared to the 5.1 weight % for not using condenser, lead to 1 in waste stream using method according to this embodiment,
The loss of 3- butadiene is reduced to 0.9 weight % of the amount for the 1,3- butadiene for being fed into polymeric segment.
In another embodiment, material stream G is also subject to absorption and stripping step.In the pressure of 20 DEG C of temperature and 445kPa
Power, with the rate of 374kg/h 1,3-butadiene and 43kg/h water to absorber unit V supply the second vapor phase G, and make G with
A certain amount of mineral oil H contact.The stream J for leaving absorber unit is provided to stripper unit VI, and generating includes 8kg/h1,
The waste stream K of 3- butadiene and 43kg/h water and recyclable in polymeric segment I including 366kg/h 1,3-butadiene
Material stream L.
Cause the loss of the 1,3- butadiene in waste stream to be reduced to using method according to this embodiment and is fed into polymeric segment
1,3- butadiene amount 0.02 weight %.
Claims (15)
1. the method for producing polymer using the compound comprising at least two unsaturation carbon-carbon bond, wherein the method includes
Polymeric segment and purification section, wherein the product of the polymeric segment is subjected to including a series of purifying steps below in the purification section
It is rapid:
Vapor phase is removed from the product of the polymeric segment by flash separation, to obtain the first vapor phase and polymerizate；
Make first vapor phase through compressed and condensation process, to obtain the second vapor phase and through condensed monomer phase；
Wherein the purification step carries out in the order.
2. according to the method described in claim 1, wherein the compound comprising at least two unsaturation carbon-carbon bond is selected from fourth
Diene, pentadiene, hexadiene, heptadiene, octadiene or their combination.
3. method described in any one of -2 according to claim 1, wherein described includes the change of at least two unsaturation carbon-carbon bond
Closing object is 1,3- butadiene.
4. method according to any one of claim 1-3, wherein the compression step includes by first vapor phase
It is compressed to >=the pressure of 400kPa.
5. method according to any of claims 1-4, wherein the compression and condensation process are compressed using positive displacement
Machine carries out.
6. method according to any one of claims 1-5, wherein described be mutually recycled back into described gather through condensed monomer
Close section.
7. method according to claim 1 to 6, wherein second vapor phase is also subject to absorption step and vapour
Step is proposed to obtain second comonomer phase.
8. according to the method described in claim 7, wherein the absorption step is carried out in the pressure of >=300kPa and≤550kPa.
9. the method according to any one of claim 7-8, wherein the absorption step is in the packed column being disposed vertically point
It is carried out from device, the separator has the entrance above the filled section of the tower, wherein by with 45-55 DEG C of temperature
Mineral oil feedstock to the tower；Second vapor phase enters the entrance of the tower；And the outlet positioned at bottom, wherein from
The mineral oil of the removal containing the compound comprising at least two unsaturation carbon-carbon bond absorbed in the tower.
10. the method according to any one of claim 7-9, wherein the absorption step includes described including at least 2
The compound of a unsaturation carbon-carbon bond is absorbed in mineral oil, and wherein the stripping step includes dividing from the mineral oil
From the compound comprising at least two unsaturation carbon-carbon bond.
11. the method according to any one of claim 9-10, wherein the mineral oil is the virtue with≤20 weight %
Hydrocarbon content and according to ISO 1523 (2002) measurement >=the synthesis isoparaffin of 40 DEG C of flash-point.
12. method according to any one of claims 7-11, wherein the stripping step≤600kPa pressure and
>=45 DEG C and≤70 DEG C of temperature carries out.
13. the method according to any one of claim 7-12, wherein the stripping step is in the packed column being disposed vertically
It is carried out in separator, the separator is in the bottom of the tower equipped with reboiler.
14. the method according to any one of claim 7-13, wherein the second comonomer is mutually recycled back into described gather
Close section.
15. method described in any one of -14 according to claim 1, wherein >=95 weight % are introduced to the polymeric segment
The monomer comprising at least two unsaturation carbon-carbon bond be converted to the polymerizate.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP16187196.7 | 2016-09-05 | ||
| EP16187196.7A EP3290445B1 (en) | 2016-09-05 | 2016-09-05 | Process for the production of a polymer using a compound comprising at least 2 unsaturated carbon-carbon bonds |
| PCT/EP2017/071029 WO2018041654A1 (en) | 2016-09-05 | 2017-08-21 | Process for the production of a polymer using a compound comprising at least 2 unsaturated carbon-carbon bonds |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109661408A true CN109661408A (en) | 2019-04-19 |
| CN109661408B CN109661408B (en) | 2021-07-09 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201780054001.6A Active CN109661408B (en) | 2016-09-05 | 2017-08-21 | Method for producing polymers using compounds containing at least 2 unsaturated carbon-carbon bonds |
Country Status (4)
| Country | Link |
|---|---|
| US (1) | US10899854B2 (en) |
| EP (1) | EP3290445B1 (en) |
| CN (1) | CN109661408B (en) |
| WO (1) | WO2018041654A1 (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0887379A1 (en) * | 1997-06-24 | 1998-12-30 | Borealis A/S | Process and apparatus for preparing propylene homopolymers and copolymers |
| WO2013135563A1 (en) * | 2012-03-16 | 2013-09-19 | Ineos Europe Ag | Process |
| EP2711350A1 (en) * | 2011-05-19 | 2014-03-26 | Asahi Kasei Chemicals Corporation | Method for manufacturing conjugated diolefin and manufacturing device therefor |
| CN103965380A (en) * | 2013-01-30 | 2014-08-06 | 中国石油化工股份有限公司 | Production method and device capable of reducing polypropylene ash |
| CN105085976A (en) * | 2014-04-22 | 2015-11-25 | 中国石油化工股份有限公司 | Method for recovering isoprene monomer and method for preparing polyisoprene |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4602083A (en) | 1985-01-10 | 1986-07-22 | Rohm And Haas Company | Coagulation process |
| EP2222718B1 (en) | 2007-12-21 | 2016-09-07 | Lubrizol Advanced Materials, Inc. | Olefin acrylate emulsion copolymerization |
| US8372924B2 (en) * | 2010-01-14 | 2013-02-12 | Exxonmobil Chemical Patents Inc. | Processes and apparatus for continuous solution polymerization |
| KR101777463B1 (en) | 2014-09-03 | 2017-09-12 | 주식회사 엘지화학 | Method for preparing resin powders and integral floculator for the same |
-
2016
- 2016-09-05 EP EP16187196.7A patent/EP3290445B1/en active Active
-
2017
- 2017-08-21 CN CN201780054001.6A patent/CN109661408B/en active Active
- 2017-08-21 US US16/330,314 patent/US10899854B2/en active Active
- 2017-08-21 WO PCT/EP2017/071029 patent/WO2018041654A1/en active Application Filing
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0887379A1 (en) * | 1997-06-24 | 1998-12-30 | Borealis A/S | Process and apparatus for preparing propylene homopolymers and copolymers |
| EP2711350A1 (en) * | 2011-05-19 | 2014-03-26 | Asahi Kasei Chemicals Corporation | Method for manufacturing conjugated diolefin and manufacturing device therefor |
| WO2013135563A1 (en) * | 2012-03-16 | 2013-09-19 | Ineos Europe Ag | Process |
| CN103965380A (en) * | 2013-01-30 | 2014-08-06 | 中国石油化工股份有限公司 | Production method and device capable of reducing polypropylene ash |
| CN105085976A (en) * | 2014-04-22 | 2015-11-25 | 中国石油化工股份有限公司 | Method for recovering isoprene monomer and method for preparing polyisoprene |
Also Published As
| Publication number | Publication date |
|---|---|
| EP3290445A1 (en) | 2018-03-07 |
| US10899854B2 (en) | 2021-01-26 |
| WO2018041654A1 (en) | 2018-03-08 |
| US20190225717A1 (en) | 2019-07-25 |
| EP3290445B1 (en) | 2018-10-31 |
| CN109661408B (en) | 2021-07-09 |
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